EP2623543A1 - Procédé de fabrication d'une fine poudre de polytétrafluoroéthylène - Google Patents

Procédé de fabrication d'une fine poudre de polytétrafluoroéthylène Download PDF

Info

Publication number
EP2623543A1
EP2623543A1 EP11829310.9A EP11829310A EP2623543A1 EP 2623543 A1 EP2623543 A1 EP 2623543A1 EP 11829310 A EP11829310 A EP 11829310A EP 2623543 A1 EP2623543 A1 EP 2623543A1
Authority
EP
European Patent Office
Prior art keywords
ptfe
fine powder
polymerization
aqueous dispersion
powder
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP11829310.9A
Other languages
German (de)
English (en)
Other versions
EP2623543B1 (fr
EP2623543A4 (fr
Inventor
Masayoshi Miyamoto
Taku Yamanaka
Yasuhiko Sawada
Masayuki Tsuji
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Daikin Industries Ltd
Original Assignee
Daikin Industries Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Daikin Industries Ltd filed Critical Daikin Industries Ltd
Publication of EP2623543A1 publication Critical patent/EP2623543A1/fr
Publication of EP2623543A4 publication Critical patent/EP2623543A4/fr
Application granted granted Critical
Publication of EP2623543B1 publication Critical patent/EP2623543B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J3/00—Processes of treating or compounding macromolecular substances
    • C08J3/12—Powdering or granulating
    • C08J3/16—Powdering or granulating by coagulating dispersions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B9/00—Making granules
    • B29B9/12—Making granules characterised by structure or composition
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2327/00—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen; Derivatives of such polymers
    • C08J2327/02—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen; Derivatives of such polymers not modified by chemical after-treatment
    • C08J2327/12—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen; Derivatives of such polymers not modified by chemical after-treatment containing fluorine atoms
    • C08J2327/18—Homopolymers or copolymers of tetrafluoroethylene

Definitions

  • the present invention relates to a method for manufacturing a polytetrafluoroethylene fine powder.
  • Polytetrafluoroethylene is produced in mainly two types of processes: suspension polymerization and aqueous dispersion (emulsion) polymerization.
  • Aqueous dispersion (emulsion) polymerization provides a latex, and polymer fine particles therein are aggregated and dried to obtain a powder (fine powder), which is then processed by paste extrusion after being compounded mainly with a liquid lubricant.
  • paste extrusion the compound is extruded into a form of a rod or a tube from an extruder.
  • the extruded articles are used as sealing materials without being subjected to further processing or by being rolled into a sheet without sintering (calendering), or as filter materials by being stretched into porous films, or are further sintered to be used as molded articles such as tubes, and wire-coatings.
  • PTFE aqueous dispersions When a high shear force is applied to PTFE aqueous dispersions, primary particles are aggregated and secondary particles having an average particle size of 100 to 1000 ⁇ m are formed (coagulation). It is known that in order to promote coagulation, an additive such as acids, alkalis, organic solvents is added. A secondary particle powder obtained by coagulation of PTFE aqueous dispersions is dried to give a PTFE fine powder.
  • PTFE fine powders are characterized by their fibrillating properties.
  • molded articles such as sealing materials, filters, tubes, pipes, and wire-coatings can be produced.
  • PTFE fine powders may be advantageous, some problems may also be caused such that secondary particle powders tend to be aggregated due to fibrillation and that the formed aggregates may not restore themselves to their original secondary particle powders. Because of these problems, PTFE fine powders tend to be aggregated or aggregated to be consolidated during production, transport or molding processes thereof, impairing handling characteristics thereof. The aggregates may lead to reduced molding properties and deteriorated appearance of molded articles. Thus, it is usually necessary to remove the aggregates with a sieve during production or before molding. They may lead to decreased working efficiency or productivity.
  • Patent Literature 1 discloses a method for manufacturing a fine powder having a high apparent density and excellent flowability by adding a fluorine-containing anionic surfactant to a PTFE aqueous dispersion.
  • coagulation of the PTFE aqueous dispersion is carried out by agitation using an anchor-type impeller.
  • Patent Literature 2 discloses granulation of a modified PTFE powder obtained by suspension polymerization, which is carried out in a granulation tank equipped with a cone-shaped impeller.
  • Patent Literature 3 discloses suspension polymerization in a 150-L stainless steel polymerization vessel equipped with a cone-shaped impeller.
  • Neither literature discloses, however, coagulation in a PTFE aqueous dispersion obtained by emulsion polymerization, which is carried out by agitation using a cone-shaped impeller.
  • an anchor-type impeller is used such as in Patent Literature 1, because the anchor-type impeller easier gives a large shear force enabling coagulation.
  • anchor-type impellers may cause following problems: a fine powder obtained by aggregation of primary particles tends to be broken by local shear forces during coagulation; and huge aggregates with a diameter of at least 1000 ⁇ m may be formed by further aggregation of the fine powder.
  • the fine powder broken by a high shear force has irregular shapes which are considered to deteriorate handling characteristics (compressibility, aggregate disintegration degree).
  • an object of the present invention is to provide a method for manufacturing a PTFE fine powder having superior handling characteristics.
  • the present inventors have unexpectedly found that agitation with a specific impeller, that is, a discharge flow-type impeller, during a coagulation step in the production of a PTFE fine powder improves handling characteristics of the resulting PTFE fine powder.
  • the present invention is a method for manufacturing a polytetrafluoroethylene fine powder, the method including the steps of:
  • the discharge flow-type impeller is preferably a cone-shaped impeller.
  • the discharge flow-type impeller is preferably a downward tapering cone-shaped impeller.
  • the method of the present invention allows production of a PTFE fine powder having a low compression ratio and a large aggregate disintegration degree as well as superior handling characteristics. According to the present method, the resulting PTFE fine powder has an equivalent apparent density to conventional fine powders.
  • the method of the present invention includes the step (1) of preparing an aqueous dispersion including polytetrafluoroethylene (PTFE), water and a surfactant (A).
  • PTFE polytetrafluoroethylene
  • A surfactant
  • the PTFE is fibrillatable and non-melt-fabricable.
  • the PTFE preferably has a standard specific gravity (SSG) of 2.13 to 2.23.
  • the PTFE preferably has a melting point of 325 to 347°C. The melting point is measured by differential scanning calorimetry (DSC) with the heating rate of 10°C/min.
  • the PTFE is preferably PTFE particles with an average primary particle size of 0.05 to 1 ⁇ m.
  • the PTFE may be a tetrafluoro- ethylene (TFE) homopolymer consisting solely of TFE or a modified PTFE composed of TFE and a modifying monomer.
  • the modifying monomer may be any monomer that can be copolymerized with TFE and examples thereof include perfluoroolefins such as hexafluoropropylene (HFP); chlorofluoroolefins such as chlorotrifluoroethylene (CTFE); hydrogen-containing fluoroolefins such as trifluoroethylene and vinylidene fluoride (VDF); perfluorovinyl ethers; perfluoroalkyl ethylenes; ethylene; and the like.
  • perfluorinated organic group means an organic group in which all hydrogen atoms linked to a carbon atom(s) are substituted with fluorine atoms.
  • the perfluorinated organic group may contain an ethereal oxygen atom.
  • perfluorovinyl ethers include perfluoro(alkyl vinyl ethers) (PAVE) which correspond to the above general formula (1) wherein Rf is a perfluoroalkyl group having 1 to 10 carbon atoms.
  • the perfluoroalkyl group preferably has 1 to 5 carbon atoms.
  • Examples of the perfluoroalkyl group in the above PAVE include perfluoromethyl, perfluoroethyl, perfluoropropyl, perfluorobutyl, perfluoropentyl, and perfluorohexyl groups, and the like.
  • PAVEs perfluoropropyl vinyl ether (PPVE) which has a perfluoropropyl group as the perfluoroalkyl group.
  • PPVE perfluoropropyl vinyl ether
  • Further examples of the perfluorovinylethers include the ones having the above general formula (1) in which Rf is a perfluoro (alkoxyalkyl) group having 4 to 9 carbon atoms; in which Rf is the group represented by the following formula:
  • the perfluoroalkyl ethylenes are not specifically limited and examples thereof include perfluorobutyl ethylene (PFBE), perfluorohexyl ethylene and the like.
  • the modifying monomer in the modified PTFE is preferably at least one selected from the group consisting of HFP, CTFE, VDF, PPVE, PFBE and ethylene. It is more preferably at least one selected from the group consisting of HFP and CTFE.
  • the modified PTFE preferably includes 1% by mass or less, more preferably from 0.001 to 1% by mass of the modifying monomer unit relative to total monomer units therein.
  • the modifying monomer unit is the moiety which is a part of the molecular structure of the modified PTFE and is derived from the modifying monomer.
  • the total monomer units mean the moieties which are derived from all monomers in the molecular structure of the modified PTFE.
  • the surfactant (A) is preferably at least one selected from the group consisting of anionic surfactants, fluorine-containing anionic surfactants, nonionic surfactants, and fluorine-containing nonionic surfactants, and more preferably at least one selected from the group consisting of fluorine-containing anionic surfactants and nonionic surfactants. It is still more preferably a fluorine-containing anionic surfactant.
  • the present method is still efficacious in preparing a PTFE fine powder when polymerization is carried out in the presence of any of the fluorine-containing surfactant (including fluorine-containing anionic surfactants and fluorine-containing nonionic surfactants) having 7 or less or 6 or less carbon atoms as the surfactant (A).
  • the fluorine-containing surfactant including fluorine-containing anionic surfactants and fluorine-containing nonionic surfactants having 7 or less or 6 or less carbon atoms as the surfactant (A).
  • fluorine-containing anionic surfactants examples include carboxylic surfactants, sulfonic surfactants, and the like.
  • the fluorine-containing anionic surfactants are preferably the carboxylic surfactants represented by the following general formula (i), (ii), (iii), (iv), (v), (vi), or (vii).
  • the fluorine-containing anionic surfactants may be carboxylic surfactants represented by the general formula (i): X-Rf 1 COOM 1 (i) wherein X is H, F or Cl; Rf 1 is a linear or branched fluoroalkylene group having 4 to 14, preferably 5 to 7 carbon atoms, for example, a linear or branched fluoroalkylene group having 7 carbon atoms and, inter alia, is a linear or branched perfluoroalkylene group; and M 1 is a monovalent alkali metal, NH 4 , or H.
  • Examples of the carboxylic surfactants represented by the general formula (i) include C 5 F 11 COOH, C 6 F 13 COOH, C 7 F 15 COOH, and the like, and salts thereof.
  • the fluorine-containing anionic surfactants may also be carboxylic surfactants represented by the general formula (ii): X 1 (CF 2 ) p -O-CX 2 X 3 -(CF 2 ) q -O-CX 4 X 5 -(CF 2 ) r -COOM 1 (ii) wherein X 1 , X 2 , X 3 , X 4 , and X 5 are the same or different from each other and represent H, F, or CF 3 ; M 1 is a monovalent alkali metal, NH 4 , or H; p is 1 or 2; q is 1 or 2; and r is 0 or 1.
  • fluoroether carboxylic acids represented by the general formula (ii) include CF 3 OCF(CF 3 ) CF 2 OCF(CF 3 )COONH 4 , CF 3 CF 2 OCF 2 CF 2 OCF 2 COONH 4 , CF 3 OCF 2 CF 2 CF 2 OCHFCF 2 COONH 4 , and the like.
  • the fluorine-containing anionic surfactants may also be carboxylic surfactants represented by the general formula (iii): X-(CF 2 ) m -O-(CF(CF 3 )CF 2 O) n -CF(CF 3 )COOM 1 (iii) wherein X is H, F, or Cl; m is an integer of 1 to 10, e.g. 5; n is an integer of 0 to 5, e.g. 1; and M 1 is a monovalent alkali metal, NH 4 , or H.
  • carboxylic surfactants represented by the general formula (iii) include CF 3 -O-CF(CF 3 )CF 2 O-CF(CF 3 )COOH and the like, and salts thereof.
  • the fluorine-containing anionic surfactants may also be carboxylic surfactants represented by the general formula (iv): X-(CF 2 ) m -O-(CF(CF 3 )CF 2 O) n -CHFCF 2 COOM 1 (iv) wherein X, m, n, and M 1 are as defined above.
  • the fluorine-containing anionic surfactants may also be carboxylic surfactants represented by the general formula (v): X-(CF 2 ) m -O-(CF(CF 3 )CF 2 O) n -CH 2 CF 2 COOM 1 (v) wherein X, m, n, and M 1 are as defined above.
  • the fluorine-containing anionic surfactants may also be carboxylic surfactants represented by the general formula (vi): Rf 3 OCF 2 CF 2 O(CF 2 ) p COOM 1 (vi) wherein Rf 3 is a partially-fluorinated or perfluorinated alkyl group; M 1 is a monovalent alkali metal, NH 4 , or H; and p is 1 or 2. Rf 3 is preferably an alkyl group having 1 to 3 carbon atoms.
  • Examples of the carboxylic surfactants represented by the general formula (vi) include CF 3 CF 2 OCF 2 CF 2 OCF 2 COONH 4 , CF 3 CF 2 OCF 2 CF 2 OCF 2 COOH, and the like.
  • the fluorine-containing anionic surfactants may also be the fluoroether carboxylic acids represented by the general formula (vii): Rf 4 OCHFCF 2 COOM 1 (vii) wherein Rf 4 is a linear aliphatic group or a linear aliphatic group to which one or more oxygen atoms are introduced, both aliphatic groups being partially-fluorinated or perfluorinated; and M 1 is a monovalent alkali metal, NH 4 , or H. Rf 4 is preferably an aliphatic group having 1 to 3 carbon atoms.
  • Examples of the carboxylic surfactants represented by the general formula (vii) include CF 3 OCF 2 CF 2 CF 2 OCHFCF 2 COONH 4 CF 3 OCF 2 CF 2 CF 2 OCHFCF 2 COOH, and the like.
  • At least one fluorine-containing surfactant selected from the group consisting of: the carboxylic surfactants represented by the general formula (i): X-Rf 1 COOM 1 (i) wherein X is H, F, or Cl; Rf 1 is a linear or branched fluoroalkylene group having 4 to 14, preferably 5 to 7 carbon atoms; and M 1 is a monovalent alkali metal, NH 4 , or H; the carboxylic surfactants represented by the general formula (ii): X 1 (CF 2 ) p -O-CX 2 X 3 -(CF 2 ) q -O-CX 4 X 5 -(CF 2 ) r -COOM 1 (ii) wherein X 1 , X 2 , X 3 , X 4 , and X 5 are the same or different from each other and represent H, F, or CF 3 ; M 1 is a monovalent alkali metal, NH 4 , or H
  • the nonionic surfactants which may be used as the surfactant (A) are not specifically limited so long as they are nonionic surfactants devoid of fluorine atoms.
  • examples thereof include ether-based nonionic surfactants such as polyoxyethylene alkylphenyl ethers, polyoxyethylene alkyl ethers, and polyoxyethylene alkylene alkyl ethers; polyoxyethylene derivatives such as ethylene oxide/propylene oxide block copolymers; ester-based nonionic surfactants such as sorbitan fatty acid esters, polyoxyethylene sorbitan fatty acid esters, polyoxyethylene sorbitol fatty acid esters, fatty acid esters of glycerol, and polyoxyethylene fatty acid esters; and amine-based nonionic emulsifiers such as polyoxyethylene alkylamines, alkyl alkanolamides; and the like. From the environmental point of view, nonionic surfactants which do not contain any alkyl phenol in their
  • the concentration of the surfactant (A) in the aqueous dispersion is preferably from 0.001 to 10% by mass, and more preferably from 0.005 to 1% by mass relative to the PTFE.
  • the aqueous dispersion in the step (1) can be prepared by aqueous dispersion polymerization, or by further treating the aqueous dispersion obtained by aqueous dispersion polymerization (emulsion polymerization) by techniques such as ion-exchange treatment, cloud point concentration, electroconcentration, and ultrafiltration.
  • the aqueous dispersion polymerization can be carried out by applying well-known polymerization techniques which may be carried out with batch, semi-batch, or continuous manners.
  • the above fluorine-containing anionic surfactant, the modifying monomer, a polymerization initiator, a stabilizer, a chain transfer agent, and the like can be continuously or sequentially added during the aqueous dispersion polymerization reaction depending on the desired molecular weight and properties of a target PTFE.
  • the aqueous dispersion polymerization is generally carried out for 0.5 to 50 hours.
  • the aqueous dispersion polymerization is carried out by using a polymerization initiator with agitation in an aqueous medium and in the presence of the fluorine-containing anionic surfactant in a pressure resistant reactor equipped with an agitator. After charging an aqueous medium, a chain transfer agent, the monomers and an optional stabilizer and adjusting temperature and pressure, the aqueous dispersion polymerization can be initiated by addition of the polymerization initiator.
  • the aqueous dispersion polymerization can be carried out while feeding a monomer into the aqueous medium.
  • tetrafluoroethylene TFE
  • TFE tetrafluoroethylene
  • the aqueous medium is preferably deionized, highly-purified water.
  • the fluorine-containing anionic surfactant can be fed to the polymerization reaction system by various ways. For example, the entire amount thereof may be fed to the reaction system at one time before the reaction is started, or it can be fed gradually in order to control the size of resulting particles as described in JP 44-14466 A . In order to improve the stability of the aqueous dispersion during the polymerization, it is preferably added during the polymerization sequentially or continuously.
  • the fluorine-containing anionic surfactant can be generally used, although it may depend on the type of the fluorine-containing anionic surfactant used and the desired primary particle size, in an amount selected from the range from 0.02 to 0.50% by mass relative to the aqueous medium used in the reaction.
  • a stabilizer may optionally be added.
  • the stabilizer is preferably paraffin wax, fluorine-containing oil, fluorine-containing compounds, silicone oil, and the like which are substantially inert in the reaction, among which paraffin wax is preferred.
  • the paraffin wax is preferably hydrocarbons having 12 or more carbon atoms and being liquid under reaction conditions, among which hydrocarbons having 16 or more carbon atoms are more preferred.
  • the melting point thereof is preferably from 40 to 65°C, more preferably from 50 to 65°C.
  • the paraffin wax is preferably used in an amount corresponding to from 1 to 12% by mass, and more preferably from 2 to 8% by mass of the aqueous medium.
  • a buffering agent such as ammonium carbonate and ammonium phosphate may be added.
  • the polymerization initiator for the emulsion polymerization may be the one conventionally used in polymerization of TFE.
  • the polymerization initiator for the emulsion polymerization is preferably radical polymerization initiators, redox-type polymerization initiators, and the like.
  • the amount of the polymerization initiator is preferably low because the SSG of the resulting TFE polymer can be decreased, an extremely low amount tends to cause a reduced polymerization rate and an extremely high amount tends to cause an increased SSG of the resulting TFE polymer.
  • the radical polymerization initiator examples include water-soluble peroxides and the like, among which persulfates such as ammonium persulfate and potassium persulfate; permanganates such as potassium permanganate; and water-soluble organic peroxides such as disuccinic acid peroxide are preferred with ammonium persulfate being more preferred.
  • the amount of the radical polymerization initiator may be appropriately selected according to the polymerization temperature and a target SSG, and is preferably 1 to 100 ppm, and more preferably from 1 to 20 ppm of the mass of the aqueous medium generally used.
  • a TFE polymer having a low SSG can be obtained by adding a radical scavenger during the polymerization reaction.
  • radical scavenger examples include unsubstituted phenols, polyhydric phenols, aromatic hydroxy compounds, aromatic amines, quinone compounds, and the like, among which hydroquinone is preferred.
  • the radical scavenger is preferably added before the polymerization of 50% by mass, and more preferably 30% by mass of the whole amount of TFE to be consumed during the polymerization reaction is completed, in order to obtain PTFE having a low SSG.
  • the amount of the radical scavenger is preferably 0.1 to 10 ppm of the aqueous medium generally used.
  • the redox-type polymerization initiator examples include a combination of a water-soluble oxidizing agent such as permanganates, e.g. potassium permanganate, persulfates, and bromates, and a reducing agent such as sulfites, bisulfites, oxalic acid, iron (II) chloride, and diimine. Among them, the combination of potassium permanganate and oxalic acid is preferred.
  • a TFE polymer having a low SSG and high breaking strength can be obtained.
  • the amount of the redox polymerization initiator can be appropriately selected according to the polymerization temperature and a target SSG, and preferably corresponds to 1 to 100 ppm of the mass of the aqueous medium generally used.
  • addition of either of the oxidizing agent and reducing agent, preferably the oxidizing agent is preferably halted in the middle of the polymerization reaction. The addition is preferably halted before the polymerization of 50% by mass, more preferably 30% by mass of the whole amount of TFE to be consumed during the polymerization reaction is completed.
  • the aqueous dispersion polymerization is preferably carried out in the presence of a dicarboxylic acid in an amount of 30 to 200 ppm relative to the aqueous medium, in order to reduce the amount of coagulated matter formed during polymerization reaction.
  • the dicarboxylic acid may be added prior to the initiation of the polymerization reaction or during the polymerization reaction.
  • the dicarboxylic acid is preferably the one represented by the general formula: HOOCRCOOH, wherein R is an alkylene group having 1 to 5 carbon atoms.
  • succinic acid, malonic acid, glutaric acid, adipic acid and pimelic acid are more preferred with succinic acid being further preferred.
  • the modifying monomer may be one intended to adjust the molding properties, extruding pressure and transparency and mechanical strength of molded articles.
  • a chain transfer agent may also be added in order to adjust the molecular weight and extrusion pressure.
  • the chain transfer agent include hydrogen; hydrocarbons such as methane, ethane, and propane; halogenated hydrocarbons such as CH 2 CF 2 , CH 3 Cl, CH 2 Cl 2 , and C 2 H 3 Cl 2 F; and water-soluble organic compounds such as methanol and ethanol. It may be added at the beginning of the polymerization or during the polymerization depending on the purposes of addition thereof. It may be added at one time, sequentially or continuously.
  • the polymerization conditions such as temperature and pressure in the aqueous dispersion polymerization are not specifically limited and can be appropriately selected according to the amount of TFE used, the type and amount of the modifying monomer (s), the type and amount of the polymerization initiator(s), productivity, or the like.
  • the temperature during the polymerization is preferably from 5 to 100°C, and more preferably from 50 to 90°C.
  • the pressure during the polymerization is preferably from 0.1 to 3.9 MPa.
  • the polymerization reaction can be stopped by terminating the agitation when the concentration of the polymer latex produced reaches 20 to 45% by mass and discharging the monomers from the system.
  • the aqueous dispersion prepared in the step (1) may be diluted with water to a polymer concentration of 10 to 20% by mass.
  • the steps (1) and (2) may be continuously performed.
  • the step (2) can be performed by agitating the aqueous dispersion prepared in the step (1) with a discharge flow-type impeller to coagulate polytetrafluoroethylene in the aqueous dispersion.
  • the primary particles are destabilized to aggregate, and simultaneously entrain the air, so that they are separated from water to give the PTFE fine powder (see Fluororesin Handbook ("Fusso Jushi Handbook"), ed. Takaomi Satokawa ).
  • the aggregate of the primary particles (fine powder) collected from the aqueous dispersion, i.e. the PTFE fine powder obtained by coagulation, has a large specific surface area as well as fibrillating properties.
  • the powder obtained by granulating a powder obtained by suspension polymerization of TFE has a small specific surface area and has poor fibrillating properties.
  • the step of agitating the aqueous dispersion of PTFE primary particles to effect coagulation is substantially different from the step of granulating a PTFE powder obtained by suspension polymerization both in terms of the objects to be agitated (materials) and of the products.
  • the discharge flow-type impeller can create an axial flow which allows the fine powder which has been rendered to be water-repellent by coagulation, to be easily entrained in water. Consequently, the fine powder becomes resistant to disruption and tends to be rolled on container walls. Thus, the fine powder is less compressed, so that aggregates of the fine powder may be easily disintegrated. In addition, the resulting powder may have a narrow shape distribution as shown in the photograph of Fig. 6 .
  • the discharge flow-type impeller may be a cylinder-shaped or cone-shaped (truncated circular cone) impeller provided therein with a component that causes a flow as a shaft rotates.
  • the component that induces a flow by agitation may be a conventional impeller of a paddle-, anchor-, ribbon-, or propeller-type, or the like, or may be a flat plate directly connected to the cylinder or cone.
  • the cylinder or cone when rotated, allows the component or directly connected plate for inducing a flow to create an axial flow, thereby agitating the content.
  • the discharge flow-type impeller may be one in which guide plate(s) or a guide cylinder is/are installed around such an impeller as described above.
  • the shape and number of the guide plates are not specifically limited.
  • the guide cylinder preferably has a cylinder shape or truncated circular cone shape (cone).
  • the guide plate (s) or guide cylinder allow (s) the impeller to create an axial flow, thereby agitating the content.
  • the discharge flow-type impeller is preferably any of the cone-shaped impellers shown in Fig. 4 .
  • cone-shaped impellers examples include an upward tapering cone-shaped impeller, a downward tapering cone-shaped impeller, a frontal coupling cone-shaped impeller, a double cone-shaped impeller having a disc saw and the like.
  • Fig. 4 is a schematic view of examples of cone-shaped impellers, in which (a) is an upward tapering cone-shaped impeller, (b) is a downward tapering cone-shaped impeller, (c) is a frontal coupling cone-shaped impeller, and (d) is a double cone-shaped impeller having a disc saw.
  • downward type is more preferred.
  • a person skilled in the art can appropriately select the rotational speed of the agitation based on the size of containers, the shape of impellers and structure of baffle plates. It is well-known to a person skilled in the art that the agitation in the step (2) is generally needed to be more vigorous than the agitation in the aqueous dispersion polymerization. In general, when a strong shear force is applied to aqueous dispersions, primary PTFE particles are aggregated to form a wet powder in water via a state of slurry. The wet powder then becomes water repellent and is separated from water.
  • the rotational speed of the agitation is not limited, but may be generally from 50 to 1000 rpm.
  • the step (2) is also preferably the one in which coagulation is initiated by starting agitation after or at the same time of addition of a coagulant.
  • the coagulant is preferably at least one selected from the group consisting of inorganic acids, inorganic salts and water-soluble organic compounds.
  • the inorganic acids include hydrochloric acid, sulfuric acid, nitric acid, and the like.
  • the inorganic salts include potassium nitrate, sodium nitrate, ammonium carbonate, sodium carbonate, aluminium nitrate, aluminium sulfate, magnesium nitrate, magnesium sulfate, ammonium hydrogen carbonate, sodium hydrogen carbonate, and the like.
  • the water-soluble organic compounds include methanol, acetone, ethanol and the like.
  • the pH may optionally be adjusted.
  • the temperature and specific gravity of the aqueous dispersion are preferably adjusted to from 0 to 80°C and from 1.03 to 1.20, respectively.
  • a pigment for colouring and a filler for imparting conductivity and improved mechanical properties can also be added.
  • a surfactant (B) may be added during the step (2).
  • the step (2) may include the steps of (2-1) initiating coagulation of polytetrafluoroethylene in the aqueous dispersion by agitating the aqueous dispersion with a discharge flow-type impeller; (2-2) adding the surfactant (B) after (2-1); and (2-3) terminating the coagulation after (2-2).
  • surfactant (B) examples include fluorine-containing surfactants such as fluorine-containing anionic surfactants, fluorine-containing nonionic surfactants, fluorine-containing cationic surfactants, and fluorine-containing betaine surfactants; and hydrocarbon-based surfactants such as hydrocarbon-based nonionic surfactants and hydrocarbon-based anionic surfactants.
  • fluorine-containing surfactants such as fluorine-containing anionic surfactants, fluorine-containing nonionic surfactants, fluorine-containing cationic surfactants, and fluorine-containing betaine surfactants
  • hydrocarbon-based surfactants such as hydrocarbon-based nonionic surfactants and hydrocarbon-based anionic surfactants.
  • fluorine-containing anionic surfactants examples include the compounds represented by the general formula (1). Specific examples may include CF 3 (CF 2 ) 6 COONH 4 , CF 3 (CF 2 ) 7 COONa, H(CF 2 CF 2 ) 4 COONH 4 , and the like.
  • R 1 is F or CF 3 ;
  • R 2 is H, F, or CF 3 , n is an integer of 4 to 20;
  • m is 0 or an integer of 1 to 6; and
  • R 3 is COOM or SO 3 M, wherein M is H, NH 4 , Na, K, or Li.
  • fluorine-containing nonionic surfactants examples include the compounds represented by the general formula (2).
  • R 1 , R 2 , n and m are as defined above; k is 0 or 1; R 4 is H, CH 3 , or OCOCH 3 ; and R 5 is (OCH 2 CH 2 ) p OR 6 , wherein p is 0 or an integer of 1 to 50; and R 6 is H, an alkyl group having 1 to 20 carbon atoms, or an aromatic group having 6 to 26 carbon atoms.
  • fluorine-containing cationic surfactants examples include the compounds represented by the above general formula (2), wherein R 5 is the group represented by the formula (3).
  • fluorine-containing betaine surfactants examples include the compounds represented by the above general formula (2), wherein R 5 is the group represented by the formula (4).
  • hydrocarbon-based nonionic surfactants examples include polyoxyethylene alkyl ethers, polyoxyethylene alkyl esters, polyoxyethylene alkylphenyl ethers, sorbitan alkylates, polyoxyethylene sorbitan monoalkylates, and the like.
  • hydrocarbon-based anionic surfactants examples include alkyl carboxylates, alkyl sulfonates, alkyl sulfates, alkyl benzene sulfonates, alkyl phosphonates, alkyl phosphates, and the like.
  • the surfactant (B) is preferably a nonionic surfactant and more preferably a hydrocarbon-based nonionic surfactant because it can contribute to effects with a small amount.
  • the amount of the surfactant (B) used is preferably 1 ppm to 10% by mass relative to the polymer solid matter in the PTFE aqueous dispersion.
  • the lower limit of the amount of the surfactant (B) used is more preferably 50 ppm and the upper limit is more preferably 10000 ppm.
  • the surfactant (B) is preferably added after the primary particles of the PTFE are aggregated to form a slurry. If the surfactant is entrained in the fine powder, reduction of the effects of addition of the surfactant and coloration of the fine powder and molded articles tend to occur. However, when the surfactant (B) is added at this time, the surfactant in a small amount can deliver desired effects of the present invention. Due to the same reason, the surfactant (B) is more preferably added after the wet powder of the PTFE is formed. It is preferably added immediately before or after the wet powder becomes water repellent and is separated from water. It is more preferable that it is added immediately before the wet powder becomes water repellent and is separated from water.
  • the coagulation can be terminated by halting the agitation.
  • the coagulation is preferably terminated after confirming that the resulting liquid is no longer in a slurry state and the water phase is transparent enough to see through.
  • the coagulation is preferably terminated after the agitation is continued for 30 seconds or more, preferably 1 min or more, and more preferably 3 min or more after water is separated (after water is repelled).
  • the method of the present invention includes the step (3) of collecting a wet powder of the PTFE.
  • the wet powder of the polytetrafluoroethylene can be collected by filtering off the wet powder of the PTFE from the mixture of the PTFE coagulation particles, water, and the surfactant (B), obtained in the step (2).
  • the method of the present invention may include the step of washing the wet powder of the PTFE obtained in the step (2).
  • the washing can be carried out by adding water and the surfactant (B) to the wet powder, keeping agitation until the PTFE particles repel water, and collecting the wet powder of the PTFE.
  • the handling characteristics of the PTFE fine powder can be further improved when the above agitation is carried out at 30 to 90°C.
  • the temperature for the above agitation is more preferably 30 to 60°C.
  • the method of the present invention includes the step (4) of drying the wet powder of the PTFE.
  • the drying is preferably carried out with little flow of the wet powder of the PTFE and by heating means such as hot air, which can be combined with reduced pressure or vacuum.
  • the temperature for drying may be below the melting point of the polymer and is usually suitable in the range of 100 to 300°C.
  • the drying temperature is preferably 180°C or more and below 300°C.
  • the drying conditions may affect paste extrusion performances.
  • the paste extrusion pressure tends to be increased with increased drying temperature.
  • the friction of the powder, especially at high temperature, is liable to cause adverse effects on the properties of the fine powder because the fine powder is easily fibrillated with a small shear force and loses its original particle structures to result in decreased paste extrusion performances.
  • the method of the present invention makes it possible to produce PTFE fine powders having the following properties:
  • SSG standard specific gravity
  • the apparent density is measured in conformity with JIS K6892.
  • the average particle size is measured in conformity with JIS K6891.
  • the compression ratio is measured at 25°C in accordance with the procedures (1) to (6) shown below:
  • the aggregate disintegration degree with 50-sec vibration is measured at 25°C according to the following procedures (1) to (7):
  • the extrusion pressure at a reduction ratio of 1500 is measured according to the following procedures:
  • the PTFE fine powder (50 g) and 10.25 g of an extrusion aid, hydrocarbon oil (trade name: ISOPAR G, Exxon Mobil Corporation) were mixed in a glass bottle and aged at room temperature (25 ⁇ 2°C) for 1 hour.
  • the mixture was charged in an extrusion die (reduction angle: 30°; equipped with an orifice (diameter: 0.65 mm, length: 2 mm) on its lower end) equipped with a cylinder (inner diameter: 25.4 mm).
  • a load of 1.2 MPa was applied to a piston in the cylinder and maintained for 1 min, immediately followed by extrusion of the mixture from the orifice at room temperature at a ram speed of 20 mm/min to obtain a rod-shaped material.
  • the pressure to the mixture is measured in a period in which the pressure is stable in the latter half of the extrusion. This pressure is divided by the cross-sectional area of the cylinder, and the obtained value is used as the extrusion pressure.
  • the modifier content in a polymer was determined from infrared absorption spectral bands of a polymer sample.
  • the compression ratio was measured on Powder Tester (Hosokawa Micron Corporation) at 25°C.
  • Figs. 1 to 3 give an overview of the measurement of the compression ratio.
  • a round-shaped powder paper (diameter: 50 mm) was placed at the bottom of a SUS cylindrical cup 2 (inner diameter: 50 mm (measured value: 51.7 mm), volume: 150 ml).
  • the inner side surface of the cup was also covered with a powder paper.
  • the PTFE fine powder 1 was sieved with a 10-mesh sieve, and 50 g of the material passing through the sieve was sampled and placed in the cylindrical cup 2 as shown in Fig. 1 .
  • the surface of the powder was smoothened and covered with a round-shaped powder paper (diameter: 50 mm).
  • a weight 3 (a cylinder having a diameter of 50 mm, weight: 330 g) was placed on the powder paper, and was tapped for 20 times on Powder Tester (tapping stroke: 20 mm). After tapping, a cylindrical cake 4 of the PTFE fine powder was taken out from the cylindrical cup 2 and the height thereof was measured with a calliper, as shown in Fig. 3 . The apparent density was calculated from the cross-section area and height of the cake.
  • the aggregate disintegration degree was measured at 25°C.
  • the vibration strength was preliminarily adjusted so that the vibration scale of 5.5 corresponds to the amplitude of 1 mm.
  • the cylindrical cake 4 was placed on a 8-mesh sieve 5 and subjected to vibration on Powder Tester (Hosokawa Micron Corporation) (vibration scale: 4.5).
  • the aggregate disintegration degree is preferred to be high, which indicated that the powder is more easily unraveled and better in handling characteristics.
  • a PTFE fine powder (50 g) and 10.25 g of an extrusion aid, hydrocarbon oil (trade name: ISOPAR G, Exxon Mobil Corporation) were mixed in a glass bottle and aged at room temperature (25 ⁇ 2°C) for 1 hour.
  • the mixture was charged in an extrusion die (drawing angle: 30°; equipped with an orifice (diameter: 0.65 mm, length: 2 mm) on its lower end) equipped with a cylinder (inner diameter: 25.4 mm).
  • a load of 1.2 MPa was applied to a piston in the cylinder and maintained for 1 min, immediately followed by extrusion of the mixture from the orifice at room temperature at a ram speed of 20 mm/min to obtain a rod-shaped material.
  • the pressure to the mixture is measured in a period in which the pressure is stable in the latter half of the extrusion. This pressure is divided by the cross-sectional area of the cylinder, and the obtained value is used as the extrusion pressure.
  • the resulting PTFE aqueous dispersion had a solids content of 24.3% by mass, an average primary particle size of 0.32 ⁇ m, and a standard specific gravity (SSG) of 2.177.
  • the PTFE aqueous dispersion obtained in Polymerization Example 1 was combined with deionized water to adjust the specific gravity to 1.080 g/ml (25°C).
  • deionized water To a 17-L stainless steel coagulation vessel equipped with an anchor-type impeller and a baffle plate was added 8.0 L of the PTFE aqueous dispersion whose specific gravity had been adjusted, and the temperature of the liquid was controlled to 22°C.
  • 6 ml nitric acid 60%) was added and, at the same time, agitation at 400 rpm was initiated. After initiation of agitation, the aqueous dispersion underwent a change into a slurry and then a wet powder was formed.
  • Fig. 5 shows a microscope photograph of the resulting PTFE fine powder in Comparative Example 1, which has been passed through a mesh sieve of #60.
  • PTFE aqueous dispersion obtained in Polymerization Example 1 was added deionized water to adjust the specific gravity to 1.080 g/ml (25°C).
  • the adjusted PTFE aqueous dispersion (10.0 L) was placed in a 17-L stainless steel coagulation vessel equipped with a downward tapering cone-shaped impeller and a baffle plate, and the temperature of the liquid was controlled to 22°C.
  • 7.5 ml nitric acid 60%) was added and, at the same time, agitation at 600 rpm was initiated. After initiation of agitation, the aqueous dispersion underwent a change into a slurry and wet powder was formed. Agitation was then continued for 3 min.
  • the wet polymer powder was then filtered off and was charged into the coagulation vessel with 8. 5 L deionized water. The temperature was adjusted to 25°C and the polymer powder was washed twice at an agitation speed of 600 rpm. After washing, the wet polymer powder was filtered off, and left in a hot air circulation dryer at 155°C for 18 hours to give a PTFE fine powder. The average particle size, apparent density, compression ratio and aggregate disintegration degree of the resulting PTFE fine powder were determined. The results are shown in Table 1.
  • Fig. 6 shows a microscope photograph of the resulting PTFE fine powder in Example 1, which has been passed through a mesh sieve of #60.
  • a PTFE fine powder was obtained in the same manner as Example 1 except that the temperature during washing was changed to 40°C. The average particle size, apparent density, compression ratio and aggregate disintegration degree of the resulting PTFE fine powder were determined. The results are shown in Table 1.
  • a PTFE aqueous dispersion was obtained by the polymerization reaction according to Example 5 of WO 2007/119829 .
  • the resulting PTFE aqueous dispersion had a solids content of 31.4% by mass, an average primary particle size of 0.35 ⁇ m, and a standard specific gravity (SSG) of 2.160.
  • a PTFE fine powder was obtained in the same manner as Comparative Example 1 except that the PTFE aqueous dispersion obtained in Polymerization Example 2 was used in lieu of the PTFE aqueous dispersion obtained in Polymerization Example 1 and that the temperature during coagulation and the temperature during drying were changed to 21°C and 210°C, respectively.
  • the average particle diameter, apparent density, compression ratio and aggregate disintegration degree of the resulting PTFE fine powder were determined. The results are shown in Table 1.
  • a PTFE fine powder was obtained in the same manner as in Example 1 except that the PTFE aqueous dispersion obtained in Polymerization Example 2 was used in lieu of the PTFE aqueous dispersion obtained in Polymerization Example 1, that the temperature during coagulation was changed to 21°C, and that the temperature during drying was changed to 210°C.
  • the average particle diameter, apparent density, compression ratio and aggregate disintegration degree of the resulting PTFE fine powder were determined. The results are shown in Table 1.
  • an aqueous solution of 12.3 mg ammonium persulfate in 20 g deionized water and an aqueous solution of 180 mg disuccinic acid peroxide in 20 g deionized water were pressed therein with TFE and the inner pressure of the autoclave was brought to 0.78 MPa.
  • the reaction proceeded at an elevated rate, while the reaction temperature and agitation were maintained at 85°C and 280 rpm, respectively.
  • the inner pressure of the autoclave was always kept at 0.78 MPa with the continuous feed of TFE.
  • PTFE aqueous dispersion had a solids content of 32.2% by mass, an average primary particle size of 0.24 ⁇ m, a standard specific gravity (SSG) of 2.177, and an amount of the modifying CTFE units in the polymer of 0.23% by weight.
  • a PTFE fine powder was obtained in the same manner as in Comparative Example 1 except that the PTFE aqueous dispersion obtained in Polymerization Example 3 was used in lieu of the PTFE aqueous dispersion obtained in Polymerization Example 1, that the temperature of coagulation was changed to 30°C, and that nitric acid was not added.
  • the average particle diameter, apparent density, compression ratio and aggregate disintegration degree of the resulting PTFE fine powder were determined. The results are shown in Table 1.
  • a TFE fine powder was obtained in the same manner as Example 1 except that the PTFE aqueous dispersion obtained in Polymerization Example 3 was used in lieu of the PTFE aqueous dispersion obtained in Polymerization Example 1, that the temperature of coagulation was changed to 30 °C, that nitric acid was not added, and that the agitation time after water was repelled was changed to 1 min.
  • the average particle diameter, apparent density, compression ratio and aggregate disintegration degree of the resulting PTFE fine powder were determined. The results are shown in Table 1.
  • the production method of the present invention is suitably applicable as a method for manufacturing a PTFE fine powder having superior handling characteristics.
  • the obtained PTFE fine powder can be molded to sealing materials, filters, tubes, pipes, wire-coatings and the like by paste extrusion or calendering.
  • the obtained PTFE fine powder can also be suitably applied for materials for stretch films, materials for porous articles, processing aids, anti-drip agents, unsintered tape, binders for batteries and the like.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Dispersion Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
  • Processes Of Treating Macromolecular Substances (AREA)
  • Compositions Of Macromolecular Compounds (AREA)
EP11829310.9A 2010-09-30 2011-09-29 Procédé de fabrication d'une fine poudre de polytétrafluoroéthylène Active EP2623543B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2010223149 2010-09-30
PCT/JP2011/072453 WO2012043757A1 (fr) 2010-09-30 2011-09-29 Procédé de fabrication d'une fine poudre de polytétrafluoroéthylène

Publications (3)

Publication Number Publication Date
EP2623543A1 true EP2623543A1 (fr) 2013-08-07
EP2623543A4 EP2623543A4 (fr) 2017-05-17
EP2623543B1 EP2623543B1 (fr) 2020-01-01

Family

ID=45893194

Family Applications (1)

Application Number Title Priority Date Filing Date
EP11829310.9A Active EP2623543B1 (fr) 2010-09-30 2011-09-29 Procédé de fabrication d'une fine poudre de polytétrafluoroéthylène

Country Status (5)

Country Link
US (1) US9006333B2 (fr)
EP (1) EP2623543B1 (fr)
JP (1) JP5177271B2 (fr)
CN (1) CN103124763B (fr)
WO (1) WO2012043757A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20130184401A1 (en) * 2010-09-30 2013-07-18 Daikin Industries, Ltd. Method for manufacturing fine polytetrafluoroethylene powder
US9309335B2 (en) 2010-09-30 2016-04-12 Daikin Industries, Ltd. Process for producing polytetrafluoroethylene fine powder
US9458316B2 (en) 2010-09-30 2016-10-04 Daikin Industries, Ltd. Dripping inhibitor and resin compound

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2015129855A1 (fr) * 2014-02-27 2015-09-03 ダイキン工業株式会社 Pâte contenant du polytétrafluoroéthylène et son procédé de production
KR102387084B1 (ko) 2014-04-02 2022-04-15 미쓰비시 엔피쯔 가부시키가이샤 폴리테트라플루오로에틸렌의 유성 용제계 분산체
CN105837839B (zh) 2015-01-30 2021-02-02 三菱铅笔株式会社 聚四氟乙烯的油性溶剂系分散体以及含聚四氟乙烯的环氧树脂组合物和其固化物
JP6459598B2 (ja) * 2015-02-16 2019-01-30 ダイキン工業株式会社 予備成形体の製造方法
KR102557635B1 (ko) 2015-04-01 2023-07-20 미쓰비시 엔피쯔 가부시키가이샤 불소계 수지 함유 비수계 분산체, 불소계 수지 함유 폴리이미드 전구체 용액 조성물, 이를 이용한 폴리이미드, 폴리이미드 필름, 회로기판용 접착제 조성물 및 그 제조 방법
CN106317265B (zh) * 2015-06-26 2018-09-11 中昊晨光化工研究院有限公司 一种聚四氟乙烯分散树脂的凝聚方法
TWI725054B (zh) 2015-10-01 2021-04-21 日商三菱鉛筆股份有限公司 氟系樹脂之非水系分散體、含氟系樹脂之熱硬化樹脂組成物與其硬化物、及電路基板用接著劑組成物
CN112111031B (zh) * 2019-06-19 2021-12-03 中昊晨光化工研究院有限公司 一种悬浮法制聚四氟乙烯树脂的回收装置和回收方法
CN116217765B (zh) * 2021-12-03 2024-04-02 中昊晨光化工研究院有限公司 一种干法电极粘结剂用聚四氟乙烯分散树脂及其制备方法
WO2024034677A1 (fr) * 2022-08-10 2024-02-15 ダイキン工業株式会社 Polytétrafluoroéthylène modifié
JP2024025770A (ja) * 2022-08-10 2024-02-26 ダイキン工業株式会社 電気化学デバイス用バインダー用フッ素樹脂、電気化学デバイス用バインダー、電極合剤、電極、及び、二次電池

Family Cites Families (53)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2075628A (en) * 1932-12-09 1937-03-30 Electric Household Utilities Washer
US2593583A (en) * 1951-03-14 1952-04-22 Du Pont Method for coagulating aqueous dispersions of polytetrafluoroethylene
JPS49115190A (fr) 1973-03-10 1974-11-02
CA1045269A (fr) 1973-07-30 1978-12-26 Tai M. Chang Thermoplastiques retardateurs de la flamme et a l'epreuve des egouttements
CA1051138A (fr) 1974-08-09 1979-03-20 Victor Mark Compose de polycarbonate retardateur de la flamme
US4391935A (en) 1974-08-09 1983-07-05 General Electric Company Flame retardant polycarbonate composition
US4355126A (en) 1974-12-06 1982-10-19 General Electric Company Flame retardant, non-dripping compositions of polyphenylene ether and acrylonitrile-butadiene-styrene
AU8671075A (en) 1974-12-06 1977-05-26 Gen Electric Flame retardant, non-dripping composition of polyphenylene ether and acrylonitrile - butadiene-styrene
DE2949908A1 (de) 1979-12-12 1981-06-19 Hoechst Ag, 6230 Frankfurt Rieselfaehige sinterpulver mit verbesserten eigenschaften auf basis von tetrafluorethylen-polymeren und verfahren zu deren herstellung
DE3322260A1 (de) 1983-06-21 1985-01-03 Bayer Ag, 5090 Leverkusen Formmassen mit flammwidrigen eigenschaften
DE3420002A1 (de) 1984-05-29 1985-12-05 Bayer Ag, 5090 Leverkusen Tetrafluorethylenpolymerisat enthaltende polymerisatpulverkompositionen
EP0174493B1 (fr) 1984-08-17 1988-05-25 Bayer Ag Masses à mouler résistant à la flamme
DE3442281A1 (de) 1984-11-20 1986-05-22 Bayer Ag, 5090 Leverkusen Verfahren zur herstellung von tetrafluorethylenpolymerisathaltigen, flammwidrigen polycarbonatformmassen
DE3516807A1 (de) 1985-05-10 1986-11-13 Bayer Ag, 5090 Leverkusen Flammwidrige, schlagzaehe polycarbonat-formmassen
US4999115A (en) * 1985-08-19 1991-03-12 Peterson Filters Corporation Method and apparatus for use in separating solids from liquids
EP0286965B1 (fr) 1987-04-17 1992-05-27 Bayer Ag Masses à mouler de polycarbonate, antistatiques et résistantes à la flamme
DE3819081A1 (de) 1988-06-04 1989-12-07 Bayer Ag Flammwidrige, schlagzaehe polycarbonat-formmassen
JP2701434B2 (ja) * 1989-03-14 1998-01-21 ダイキン工業株式会社 ポリテトラフルオロエチレンの湿潤パウダーの連続製造法
DE4102104A1 (de) 1991-01-25 1992-07-30 Bayer Ag Flammgeschuetzte, nicht tropfende polyamidformmassen
JPH05214184A (ja) 1992-02-07 1993-08-24 Mitsubishi Rayon Co Ltd 加工性の改良されたポリプロピレン樹脂組成物
JPH05287151A (ja) 1992-04-08 1993-11-02 Asahi Glass Co Ltd 成形用ポリテトラフルオロエチレン組成物、その製造方法および成形加工方法
JPH06306212A (ja) 1993-04-23 1994-11-01 Kanegafuchi Chem Ind Co Ltd ポリオレフィン系樹脂組成物
JP3274933B2 (ja) 1994-05-31 2002-04-15 鐘淵化学工業株式会社 ポリオレフィン系樹脂組成物の製法
JP3446377B2 (ja) 1995-03-17 2003-09-16 ダイキン工業株式会社 ポリテトラフルオロエチレンファインパウダーおよびその製法
FR2733504A1 (fr) 1995-04-28 1996-10-31 Gen Elec Plastics Abs Euro Bv Nouveaux alliages polymeres a base de polymerisat comprenant des motifs de derives de tetrafluoroethylene, procede de fabrication, articles obtenus a partir de tels alliages et utilisation de ces alliages dans des compositions polymeres
WO1997017382A1 (fr) 1995-11-09 1997-05-15 Daikin Industries, Ltd. Poudre fine de polytetrafluoroethylene, sa fabrication et son utilisation
JPH1077378A (ja) 1996-09-02 1998-03-24 Daikin Ind Ltd ドリップ防止剤および難燃性樹脂組成物
JP3931382B2 (ja) 1996-09-18 2007-06-13 ダイキン工業株式会社 ポリテトラフルオロエチレン粉末及びその製造方法
JP3152284B2 (ja) 1997-03-17 2001-04-03 ダイキン工業株式会社 変性ポリテトラフルオロエチレン粒状粉末
JPH10310707A (ja) 1997-05-13 1998-11-24 Mitsubishi Rayon Co Ltd 熱可塑性樹脂組成物
US6422736B1 (en) * 2000-06-21 2002-07-23 Eastman Kodak Company Scalable impeller apparatus for preparing silver halide grains
FR2841403B1 (fr) * 2002-06-21 2004-10-15 Renault Sa Procede de pilotage electronique d'un dispositif de commande d'un actuateur piezo-electrique ultrasonore
KR100991167B1 (ko) * 2003-02-19 2010-11-02 듀폰-미쯔이 플루오로케미칼 가부시끼가이샤 열용융성 불소 수지 복합체 조성물의 제조 방법 및 열용융성 불소 수지 복합체 조성물
WO2004076539A1 (fr) 2003-02-28 2004-09-10 Daikin Industries, Ltd. Poudre granulee de polyetrafluoroethylene a faible masse moleculaire et poudre de polyetrafluoroethylene a faible masse moleculaire et procedes de fabrication associes
JP3775420B2 (ja) 2003-02-28 2006-05-17 ダイキン工業株式会社 低分子量ポリテトラフルオロエチレン造粒粉末、低分子量ポリテトラフルオロエチレン粉末及びこれらの製造方法
US20070155891A1 (en) 2003-12-09 2007-07-05 Daikin Industries, Ltd. Water base dispersion of fluorinated polymer and process for producing the same
US7220456B2 (en) * 2004-03-31 2007-05-22 Eastman Kodak Company Process for the selective deposition of particulate material
ATE540061T1 (de) 2004-11-16 2012-01-15 Daikin Ind Ltd Feines pulver aus modifiziertem polytetrafluorethylen und formkörper aus modifiziertem polytetrafluorethylen
KR100716021B1 (ko) 2005-03-10 2007-05-08 박지호 테트라플로로에틸렌 중합체를 포함하는 현탁 입자 및 그 제조 방법
JP5391550B2 (ja) 2005-10-20 2014-01-15 旭硝子株式会社 溶融成形可能なフッ素樹脂の製造方法
CN101296950B (zh) 2005-10-26 2011-01-26 旭硝子株式会社 含氟乳化剂的残留量少的氟树脂及其制造方法
US20070142513A1 (en) * 2005-12-21 2007-06-21 Daikin Industries, Ltd. Surfactant, method of producing a fluoropolymer, fluoropolymer aqueous dispersion
EP2011804B1 (fr) 2006-04-13 2013-01-16 Daikin Industries, Ltd. Polymere de tetrafluoroethylene et dispersion aqueuse de celui-ci
JP4445983B2 (ja) * 2007-07-06 2010-04-07 シャープ株式会社 トナーの製造方法
US20110196080A1 (en) 2007-08-01 2011-08-11 Kuraray Co., Ltd. Polyamide composition
EP2267047B1 (fr) 2008-04-14 2012-01-18 Asahi Glass Company, Limited Procédé de fabrication de fine poudre de polytétrafluoroéthylène
RU2478653C2 (ru) 2008-05-21 2013-04-10 Асахи Гласс Компани, Лимитед Способ получения тонкодисперсного порошка политетрафторэтилена
BRPI0914250B1 (pt) 2008-07-03 2018-12-26 Ricoh Co Ltd composição de resina retardante de chama
EP2308927B1 (fr) 2008-07-23 2012-06-06 Mitsubishi Engineering-Plastics Corporation Composition de résine de polyester thermoplastique
WO2011055824A1 (fr) 2009-11-09 2011-05-12 旭硝子株式会社 Émulsion aqueuse de polytétrafluoroéthylène et son procédé de fabrication, dispersion aqueuse de polytétrafluoroéthylène obtenue à l'aide de l'émulsion, poudre fine de polytétrafluoroéthylène et corps expansé étiré
CN103080221B (zh) * 2010-09-30 2015-11-25 大金工业株式会社 防熔滴剂以及树脂组合物
JP5177271B2 (ja) * 2010-09-30 2013-04-03 ダイキン工業株式会社 ポリテトラフルオロエチレンファインパウダーの製造方法
WO2012043881A1 (fr) 2010-09-30 2012-04-05 Daikin Industries, Ltd. Procédé de production de poudre fine de polytétrafluoroéthylène

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2012043757A1 *

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20130184401A1 (en) * 2010-09-30 2013-07-18 Daikin Industries, Ltd. Method for manufacturing fine polytetrafluoroethylene powder
US9006333B2 (en) * 2010-09-30 2015-04-14 Daikin Industries, Ltd. Method for manufacturing fine polytetrafluoroethylene powder
US9309335B2 (en) 2010-09-30 2016-04-12 Daikin Industries, Ltd. Process for producing polytetrafluoroethylene fine powder
US9458316B2 (en) 2010-09-30 2016-10-04 Daikin Industries, Ltd. Dripping inhibitor and resin compound
US9475935B2 (en) 2010-09-30 2016-10-25 Daikin Industries, Ltd. Dripping inhibitor and resin compound

Also Published As

Publication number Publication date
JP2012092323A (ja) 2012-05-17
CN103124763B (zh) 2015-01-14
WO2012043757A1 (fr) 2012-04-05
EP2623543B1 (fr) 2020-01-01
CN103124763A (zh) 2013-05-29
US9006333B2 (en) 2015-04-14
EP2623543A4 (fr) 2017-05-17
US20130184401A1 (en) 2013-07-18
JP5177271B2 (ja) 2013-04-03

Similar Documents

Publication Publication Date Title
EP2623543B1 (fr) Procédé de fabrication d'une fine poudre de polytétrafluoroéthylène
US9309335B2 (en) Process for producing polytetrafluoroethylene fine powder
EP1939222B2 (fr) Procédé de production emulsion aqueuse de polytetrafluoroethylene et poudre fine de polytetrafluoroethylene et materiau poreux produit a partir de celle-ci
EP2415788B1 (fr) Poudre de polytétrafluoroéthylène de faible masse moléculaire et son procédé de préparation
JP5750375B2 (ja) フッ素化イオノマーの分散微粒子を使用する水性重合により製造されるフルオロポリマー
JP5481495B2 (ja) フッ素化イオノマーの核を有するフルオロポリマー粒子
EP2287209B1 (fr) Procédé pour la fabrication de fine poudre de polytétrafluoroéthylène
RU2478654C2 (ru) Способ получения тонкодисперсного порошка политетрафторэтилена
EP2367862A1 (fr) Polymérisation aqueuse de monomère fluoré à l'aide d'un tensio-actif éther fluoré ramifié à base d'hydrogène
CN114685706B (zh) 氟代烯烃的水分散体和氟代烯烃的共聚物的水分散体以及它们的制造方法

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20130311

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

DAX Request for extension of the european patent (deleted)
RA4 Supplementary search report drawn up and despatched (corrected)

Effective date: 20170420

RIC1 Information provided on ipc code assigned before grant

Ipc: C08J 3/16 20060101AFI20170412BHEP

Ipc: B29B 9/12 20060101ALI20170412BHEP

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS

17Q First examination report despatched

Effective date: 20180928

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: GRANT OF PATENT IS INTENDED

INTG Intention to grant announced

Effective date: 20190911

RIN1 Information on inventor provided before grant (corrected)

Inventor name: YAMANAKA TAKU

Inventor name: SAWADA YASUHIKO

Inventor name: MIYAMOTO MASAYOSHI

Inventor name: TSUJI MASAYUKI

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE PATENT HAS BEEN GRANTED

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

REG Reference to a national code

Ref country code: AT

Ref legal event code: REF

Ref document number: 1219721

Country of ref document: AT

Kind code of ref document: T

Effective date: 20200115

Ref country code: CH

Ref legal event code: EP

REG Reference to a national code

Ref country code: DE

Ref legal event code: R096

Ref document number: 602011064396

Country of ref document: DE

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

REG Reference to a national code

Ref country code: NL

Ref legal event code: FP

REG Reference to a national code

Ref country code: LT

Ref legal event code: MG4D

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200401

Ref country code: LT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

Ref country code: RS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

Ref country code: FI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

Ref country code: PT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200527

Ref country code: CZ

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200402

Ref country code: HR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

Ref country code: LV

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

Ref country code: SE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

Ref country code: BG

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200401

Ref country code: IS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200501

REG Reference to a national code

Ref country code: DE

Ref legal event code: R097

Ref document number: 602011064396

Country of ref document: DE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: ES

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

Ref country code: RO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

Ref country code: SK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

Ref country code: DK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

Ref country code: SM

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

Ref country code: EE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

REG Reference to a national code

Ref country code: AT

Ref legal event code: MK05

Ref document number: 1219721

Country of ref document: AT

Kind code of ref document: T

Effective date: 20200101

26N No opposition filed

Effective date: 20201002

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: AT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: PL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

Ref country code: SI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MC

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

REG Reference to a national code

Ref country code: BE

Ref legal event code: MM

Effective date: 20200930

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20200929

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20200930

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LI

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20200930

Ref country code: IE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20200929

Ref country code: CH

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20200930

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20200930

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: TR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

Ref country code: MT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

Ref country code: CY

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

Ref country code: AL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200101

P01 Opt-out of the competence of the unified patent court (upc) registered

Effective date: 20230525

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: IT

Payment date: 20230810

Year of fee payment: 13

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 20240816

Year of fee payment: 14

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20240806

Year of fee payment: 14

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 20240808

Year of fee payment: 14